US5440028A

US5440028A - Process for preparing purified glycolipids by membrane separation processes

Info

Publication number: US5440028A
Application number: US08/257,445
Authority: US
Inventors: Rainer Buchholz; Ulrich Fricke; Johann Mixich
Original assignee: Hoechst AG
Current assignee: Hoechst AG
Priority date: 1990-09-25
Filing date: 1994-06-08
Publication date: 1995-08-08
Anticipated expiration: 2013-03-23
Also published as: EP0550509A1; NO931093L; GR3020156T3; FI97473C; DE4030264A1; NO179074C; NO179074B; FI931274A; ATE138923T1; NO931093D0; FI97473B; DE59107901D1; JPH06501249A; WO1992005183A1; ES2088016T3; DK0550509T3; EP0550509B1; FI931274A0

Abstract

Process for preparing purified glycolipids by membrane separation processes. Glycolipids may be purified and concentrated using a membrane separation process at acid pH and employing a membrane with a cut-off size of 30,000.

Description

This application is a continuation of application Ser. No. 08/030.090 filed as PCT/EP91/01756, Sep. 14, 1991, now abandoned.

Glycolipids are composed of a fatty acid residue and a sugar residue. One of the best-known glycolipids is trehalose lipid (Suzuki et al., 1969, Agric. Biol. Chem., 33, 1619-1627). It is composed of the disaccharide trehalose and two β-hydroxy α-branched fatty acids (corynomycolic acid) which are esterified by hydroxyl groups of the sugar. Glycolipids that contain rhamnose and β-hydroxy fatty acids are described in EP 0 153 634. The first rhamnolipid to have its structure determined comprises two molecules of L-rhamnose and two molecules of β-hydroxydecanoic acid (Ewards and Hayashi, 1965, Arch. Biochem. Biophys., 111, 415-421).

The glycolipids known hitherto have a molecular weight between 250 and 2000, in each case depending on the sugar moiety and the fatty acid moiety. They are secreted into the surrounding nutrient medium by bacteria, for example, and can be accumulated as a mixture of several different glycolipids (EP 0 153 634; Advances in Appl. Microbiol. 1980, 229-259).

Glycolipids can be used, for example, as emulsifiers, biosurfactants or stabilizers for emulsions.

The processes for purifying glycolipids are based on extraction, crystallization and chromatographic processes (EP 0 282 942; U.S. Pat. No. 4 814,272). However, large quantities of solvents accumulate in these processes. Mulligan and Gibbs (J. Chem. Tech. Biotechnol, 1990, 47, 23-29) describe an ultrafiltration process for purifying biosurfactants, such as surfactin and rhamnolipids. However, the retention ability of the membranes described in that paper decreases with increasing pore size. In the case of membranes with a cut-off size of 30,000, this leads to glycolipid losses of more than 77%.

It has now been found, surprisingly, that, at acid pH, glycolipids are virtually completely retained by a membrane that has a cut-off size for molecules with a molecular weight of more than 30,000.

The invention consequently relates to a process for preparing purified glycolipids which is characterized in that the purification is carried out using a membrane separation process at acid pH with a membrane which has a cut-off size for molecules with a molecular weight of more than 30,000.

The invention is described in detail below, in particular in its preferred embodiments.

Glycolipids can occur in plants or bacteria (Lehninger, Biochemistry, 1977; Syldakt et al., Z. Naturforschung, 40 c, 1985, 51-67). Fermentations preferably come into consideration for preparing glycolipids. For this purpose, the microorganisms are cultured in a manner known per se. The glycolipids which are secreted into the culture medium are, for example, purified at the end of the fermentation using the membrane separation process according to the invention, preferably ultrafiltration. The ultrafiltration can be carried out, for example, with equipment using plates, tubes, capillary tubes, spiral membranes or hollow fibers, containing membranes with a cut-off size of 30,000 to 300,000. Membranes are preferably employed with a cut-off size of 100,000 to 200,000. The cut-off size relates to the molecular weight of the molecules to be retained and means that substances with a molecular weight greater than the stated value are retained. Polysulfones, polyamides or cellulose acetates may be used as the membrane material. The glycolipids are retained by the membrane and can be processed further after the purification.

The membrane separation process according to the invention is carried out at an acid pH, preferably at a pH of 1 to 5,particularly preferably at a pH of 2 to 4. Adjustment of pH is effected, if necessary, using an acid or an alkali. Hydrochloric acid, sulfuric acid, acetic acid, citric acid, sodium hydroxide or sodium carbonate may be used, for example.

The process according to the invention is advantageously employed for the purification of rhamnolipids. The purification of α-L-rhamnopyranosyl-β-hydroxydecanoic acid,

2-O-α-L-rhamnopyranosyl-α-L-rhamnopyranosyl-β-hydroxydecanoic acid,

2-O-α-L-rhamnopyranosyl-α-L-rhamnopyranosyl-β-hydroxydecanoyl-β-hydroxydecanoic acid or

α-L-rhamnopyranosyl-β-hydroxydecanoyl-β-hydroxydecanoic acid is particularly preferred.

The purification of glycolipids with an ultrafiltration system can be carried out batchwise or continuously. The temperature of the filtration solution is kept between 0° C. and 70° C., preferably between 18° C. and 40° C.

The velocity of flow of the fluid over the membrane is kept between 2 and 7 m/s, preferably between 5 and 6 m/s. The excess pressure of the fluid at the input to the filtration appliance amounts to between 3 and 6 bar. The pressure drop over the filtration distance lies between 0.5 and 3.5 bar.

The membrane separation process according to the invention may naturally be used not only for purifying glycolipids but also for concentrating them.

Example 1

Pseudomonas spec. DSM 2874 was cultured under aerobic conditions in a nutrient solution using paraffin S (89% tetradecane, 9% pentadecane) as carbon source, in accordance with German Patent 3 405 664. The fermentation was effected at a pH of 6.6 and 7.2, and at 30° C. with an aeration rate of 0.2 V/V/m. The fermentation had finished after 7 days. The fermentation solution contained a rhamnose-lipid mixture with an L-rhamnose component of 2.5 g/l.

EXAMPLE 2

The fermentation solution obtained from Example 1 was adjusted to pH 3 with sulfuric acid and subsequently concentrated in a modular tube-ultrafiltration system (Bottcher, Austria). The following operational parameters were maintained:

______________________________________                                    
Input pressure        5      bar                                          
Output pressure       1.5    bar                                          
Temperature           35°                                          
                             C.                                           
Flow-over velocity    5      m/s                                          
Filtration performance                                                    
                      200    l/h                                          
Concentration factor  3.9                                                 
Initial volume        18.6   m.sup.3                                      
Final volume          4.8    m.sup.3                                      
______________________________________

After the concentration, the concentrate contained a rhamnose-lipid mixture with an L-rhamnose component of 9.75 g/l.

EXAMPLE 3

The concentrated fermentation solution obtained from Example 2 was desalted with water by diafiltration at pH 3 and constant volume. A modular tube-ultrafiltration system (Bottcher, Austria) was used for this purpose. The UF-PS-100 polysulfone membrane, from Kalle-Albert, Wiesbaden, had a cut-off size of 100,000. The following operational parameters were maintained:

______________________________________                                    
Input pressure        5      bar                                          
Output pressure       1.5    bar                                          
Temperature           35°                                          
                             C.                                           
Flow-over velocity    5      m/s                                          
Filtration performance                                                    
                      59     l/m.sup.2 h                                  
Volume of the solution                                                    
                      4.8    m.sup.3                                      
______________________________________

The fermentation broth had a conductivity of 24.5 mS cm^-1 before desalting and 2.9 mS cm^-1 thereafter. The permeate contained 0.1 g/1 L-rhamnose.

EXAMPLE 4

For comparison, a fermentation solution containing rhamnose lipid was passed over membranes with cut-off sizes of 10,000 and 100,000, respectively:

______________________________________                                    
Operational parameters:                                                   
______________________________________                                    
Flow over              0.3    m.sup.3 /h                                  
Output pressure        4      bar                                         
Temperature            32°                                         
                              C.                                          
Membrane area          0.45   m.sup.2                                     
pH                     3                                                  
______________________________________                                    
Membrane types    Permeate Flux l/m.sup.2 h                               
______________________________________                                    
Polysulfone 10,000 D                                                      
                  Clear    0.8                                            
Polysulfone 100,000 D                                                     
                  Clear    50.0                                           
______________________________________

In both cases the retention of rhamnolipid was 99%.

Claims

We claim:

1. A process for preparing purified glycolipids wherein the purification is carried out using a membrane separation process at acid pH with a membrane which has a cut-off size of molecules with a molecular weight of more than 30,000.

2. A process according to claim 1 wherein the glycolipids are rhamnolipids.

3. A process according to claim 1 wherein the glycolipids are selected from the group consisting of α-L-rhamnopyranosyl-β-hydroxydecanoic acid, 2-O-α-L-rhamnopyranosyl-α-L-rhamnopyranosyl-β-hydroxydecanoic acid, 2-α-L-rhamnopyranosyl-α-L-rhamnopyranosyl-β-hydroxydecanoyl-β-hydroxydecanoic acid and α-L-rhamnopyranosyl-β-hydroxydecanoyl-β-hydroxydecanoic acid.

4. A process according to claim 1 wherein ultrafiltration serves as the membrane separation process.

5. A process according to claim 4 wherein an ultrafiltration membrane with a cut-off size of 30,000 to 300,000 is employed.

6. A process according to claim 5 wherein an ultrafiltration membrane with a cut-off size of 100,000 to 200,000 is employed.

7. A process according to claim 4 wherein the process is carried out at a pH of 1 to 5.

8. A process according to claim 7 wherein the process is carried out at a pH of 2 to 4.

9. A process according to claim 8 wherein the process is carried out at a temperature of 0° to 70° C.

10. A process according to claim 7 wherein the process is carried out at a temperature of 0° to 70° C.

11. A process according to claim 4 wherein the process is carried out at a temperature of 0° to 70° C.

12. A process according to claim 1 wherein the process is carried out at a pH of 1 to 5.

13. A process according to claim 12 wherein the process is carried out at a pH of 2 to 4.

14. A process according to claim 13 wherein the process is carried out at a temperature of 0° to 70° C.

15. A process according to claim 12 wherein the process is carried out at a temperature of 0° to 70° C.

16. A process according to claim 1 wherein the process is carried out at a temperature of 0° to 70° C.